WO2003064335A1 - Hybrid biological membrane reactor for the treatment of urban and industrial waste water - Google Patents

Hybrid biological membrane reactor for the treatment of urban and industrial waste water Download PDF

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Publication number
WO2003064335A1
WO2003064335A1 PCT/ES2003/000057 ES0300057W WO03064335A1 WO 2003064335 A1 WO2003064335 A1 WO 2003064335A1 ES 0300057 W ES0300057 W ES 0300057W WO 03064335 A1 WO03064335 A1 WO 03064335A1
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Prior art keywords
chamber
aerobic
sludge
anoxic
filtration
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PCT/ES2003/000057
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Spanish (es)
French (fr)
Inventor
Juan Manuel GARRIDO FERNÁNDEZ
Ramón Méndez Pampín
Vinka OYANEDEL BASÁEZ
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Universidade De Santiago De Compostela
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Priority to DE2003604456 priority Critical patent/DE60304456T2/en
Priority to EP03734736A priority patent/EP1484287B1/en
Publication of WO2003064335A1 publication Critical patent/WO2003064335A1/en

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/06—Aerobic processes using submerged filters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • DESCRIPTION Biological membrane hybrid reactor for industrial and urban wastewater treatment with organic and nitrogenous matter. It consists of three chambers: anoxic, aerobic and membrane filtration. The proposed reactor is a compact system with which very low or negligible levels of suspended solids are achieved in the purified effluent. Description of the state of the art of the main ones: A) Biological treatment technologies and processes for the elimination of nitrogen and organic pollutants; and B) Membrane bioreactor systems and hybrid reactors for wastewater treatment.
  • A) Biological wastewater treatment technologies are widely used for the elimination of organic pollutants, nitrogen and phosphorus compounds and are based on biological processes that employ cultures of microorganisms of different species, mainly bacteria, fungi, algae, protozoa and metazoans.
  • heterotrophic microorganisms are characterized by using organic compounds in their growth, both in aerobic conditions (using oxygen as an oxidizing agent) or anoxic (reducing nitrite or nitrate to gaseous nitrogen).
  • Mirifying bacteria oxidize ammonia to nitrite or nitrate, under aerobic conditions and are characterized by having a slower growth rate and lower cell production rate than heterotrophic bacteria.
  • the active sludge process developed in the United Kingdom in 1914 stands out (Andern E. and Lockett W.T. J. Soc. Chem. Ind. 33, 523 (1914)). It consists of a reactor where a suspended microbial culture is maintained in aerobic conditions and a settler to separate the treated wastewater from the microbial sludge, recirculating it to the biological system.
  • the active sludge process was initially designed for the elimination of contaminating organic matter, but later different configurations of the process were developed for the elimination of nitrogen and phosphorus compounds from wastewater. »Configurations with one or multiple reactors are usually used.
  • A.2) In biofilm or biofilm systems of immobilized microorganisms, the following stand out: 1) percolating filters, .2) rotary biological contactors and 3) submerged biological filters.
  • the percolating filters used since the XLX century, consist of a column equipped with a filling (of pebbles, stones, wooden slats, plastic support, etc.) that remains fixed and on which a formed biofilm grows by microorganisms. In the column, open at its upper and lower ends; wastewater is spread throughout the entire system by contacting wastewater, biofilms and air.
  • the main applications of percolating filters are the elimination of organic matter and the treatment of biological nitrification. Its use is not recommended when it is necessary to remove nitrogen from wastewater.
  • the rotary biological contactors are formed by a support of specific high surface plastic discs on which a biofilm grows;
  • the disks coupled to a rotating shaft, are partially submerged in the wastewater.
  • the rotation of the discs allows the correct transfer of oxygen from the air to the biofilm and facilitates the contact of the biofilm with the contaminants present in the wastewater.
  • the biodisc process originated at the Technical University of Stuttgart (Germany) in 1955 and the first scale plant industrial was launched in the US UU. in 1969. Biodisks have the same drawback as percolating filters, so they are rarely used if nitrogen needs to be removed.
  • the principle of operation of submerged biological filters is similar to that of percolating filters, although in these systems the column containing the support with residual water is completely flooded.
  • the air supply, if necessary, is guaranteed by air injection and there are also units that operate under anoxic conditions for denitrification.
  • the supports for the growth of biofilms are organic materials such as polyethylene, polystyrene, polyurethane, granular particles of expanded clay, particles of pozzolana, sand, or other materials with sizes generally between 1 and 5 mm.
  • the first biofilters on an industrial scale were developed in the 70s in France using expanded clays as support (Lazarova and Manem, Biofilms II: Process Analyzes and Applications, Editor James E. Bryers, (2000)).
  • Some of these systems use granular plastic supports, with a density slightly lower than that of water, (patents FR2707183 and WO9713727) on which a biofilm grows, which allows these supports to be easily fiuidized by introducing a gas flow into the system.
  • Submerged biofilters are very compact units that are used for various purposes: anaerobic removal, denitrification and / or aerobic oxidation of organic matter as well as nitrification of ammonia in wastewater, and have relatively high contaminant removal rates.
  • One of the most general problems for its application derives from the greater complexity - technique.
  • Hybrid systems are characterized by combining the presence of suspended biomass with immobilized biomass on a support in the same system, which allows maintaining higher concentrations of biocatalyst than those used in suspended biomass reactors, this peculiarity constitutes an advantage , since it is possible to purify wastewater in more compact hybrid equipment than the classic active sludge systems.
  • Hybrid reactors are becoming increasingly important in the purification of wastewater with organic matter and nitrogen, as they combine the robustness of active iodine systems with the greater purification capacity of biofilm systems.
  • hybrid systems are US5061368 and bibliographic references (Andreottola et al .; Münch et al .; ⁇ degaard et al .; Wat. Sci. Technol. V41, No. 4-5, (1999)) using plastic supports such as those described in patents US5458779, US5543039 and US6126829 to improve the performance of various biological reactors in which biomass grows both in suspension and in biofilms.
  • US5061368 uses a hybrid system that alternates anaerobic and chambers. anoxic, maintaining suspended biomass throughout the system and immobilized biomass in a gel cubes retained in nitrifying aerobic chambers.
  • a disadvantage of this system is that it artificially immobilizes nitrifying microorganisms in polyethylene glycol gel cubes that must be periodically replenished to replace those gel particles that break or wear out, so it is necessary to manufacture new gel cubes, not only during the commissioning stage, but also during the continuous operation of the system.
  • very high loading rates cannot be applied since they can cause the breakage of the gel cubes by increasing the growth rate of the immobilized microorganisms.
  • membranes that have been used for this purpose are microfiltration or ultrafiltration membranes made of organic or inorganic materials arranged in hollow fiber, plate or tubular modules that can be placed inside or outside the biological reactor (Günder B. and Krauth K. , Wat. Sci.
  • the present invention involves improvements in systems for the biological treatment of wastewater, in general, and hybrid reactors, in particular.
  • One of the main characteristics of the proposed hybrid reactor is to confine particles of a plastic granular support in the aerobic chamber, with a slightly lower density than that of water. This support does not break or deteriorate due to use in the system; In addition, it will not break due to the growth of the biomass in it (as can occur in systems that use immobilized microorganisms within polymer gels) since growth is limited to the surface of the plastic support. This also saves the need for a stock of gel particles with microorganisms.
  • Another advantage is the use of a filtration system of hollow fiber membranes.
  • the separation efficiency depends on the sedimentability properties of the sludge, and can worsen if high pollutant loads are applied in the system.
  • the proposed membrane filtration system makes the process of separating treated wastewater and sludge independent of sedimentability properties, so that higher loading speeds can be applied without risk of system operation problems. In addition, the possible washing of the sludge from the biological reactor is avoided.
  • membrane filtration units in the hybrid reactor makes it possible to obtain an effluent with low levels of suspended solids, which would meet the most demanding discharge requirements of this contaminant, significantly decreases the discharge of microorganisms with the effluent (including pathogens and other health vectors); In addition, it is suitable for discharges in the vicinity of areas of marine culture or fish farms and areas of water catchment used for irrigation or the production of drinking water.
  • the plastic granular support is confined with the biofilms in the aerobic chamber, using separation devices that allow the free passage of the mixing liquor, with the microorganisms in suspension between the three chambers of which the unit consists.
  • Figures 1-5 represent the hybrid biological membrane reactor:
  • Figure 1 Diagram of the reactor consisting of the three chambers: anoxic chamber (1), aerobic chamber (2), and filtration chamber (3).
  • Figure 2. Three-dimensional perspective of the reactor, showing the three chambers, the two baffle plates (7) of the aerobic chamber, wastewater recirculation channel (18) and overflow (17). The civil work has been highlighted, omitting auxiliary equipment.
  • Figure 3 Shape and arrangement of the passage of the mixing liquor (6) from the anoxic chamber (1) to the aerobic chamber (2).
  • FIG. 1 Collection wells (10 and 10 ') of the mixing liquor from the aerobic chamber (2) to the filtration chamber (3).
  • the conduit (11) is used for the transport of wastewater between the chambers.
  • FIG. 1 Section AA '(in figure 1) showing a mixing liquor delivery device from the filtration chamber to the anoxic chamber, showing the centrifugal stirrer (15), the conduit (16) and the recirculation channel ( 18).
  • Figures 1 and 2 represent the essential characteristics of the system. It consists of three cameras: anoxic chamber (1); aerobic camera, air lift type (2); and filtration chamber (3). In the three chambers microbial sludge is maintained 'suspension. In the aerobic chamber (2), a granular and rough plastic support of lower density than water is confined, on which a biofilm with a high fraction of nitrifying microorganisms grows.
  • the system incorporates in its filtration chamber (3) modules of ultrafiltration membranes of hollow fibers (12) that are used to separate the treated water from the biological sludge, recirculating the sludge of this chamber to the anoxic (1).
  • Figure 1 shows how the wastewater is introduced into the anoxic chamber (1) through the conduit located in the upper part thereof (4), the influent being mixed with the mixing liquor present in the chamber.
  • the homogeneity of the mixture formed by microorganisms in suspension and residual water is guaranteed using a suitable mechanical agitation device (5), such as a flow accelerator or mechanical agitator.
  • the biological denitrification takes place whereby part of the nitrogen anions present in the water are reduced to gaseous nitrogen, by means of the biocatalyst present, also eliminating a high fraction of the organic pollutants in the Denitrification reaction and adsorption of soluble organic compounds, so that part of the organic matter can be removed from the water that could otherwise be assimilated by the biofilms present in the aerobic chamber (2).
  • the conduction of figure 3 allows the mixing liquor to pass from the anoxic chamber (1) to the aerobic (2).
  • This passageway is formed by one or more circular section ducts (6) through which the mixing liquor from (1) to (2) circulates.
  • the design of the conduction at an angle is set in such a way that the back-mixing of the fluid between the chambers is limited and minimizes or prevents both the support entrance of the aerobic chamber (2) to the anoxic chamber (1) and the deposition of mud in the same.
  • the inclination of the inclined section of the tube with respect to the horizontal section thereof will be between 20 ° and 90 °.
  • the aerobic camera (2) is an air-lift type device in which two deflector plates or dances are installed that divide this camera into three rectangular sections (figures 1 and 2): a central section called riser or shot, which has in its lower part of diffusers through which air is distributed, and two sections on the sides called downspouts or down-comers.
  • a rough granular plastic support is confined with a density of 5% to 15% less than that of water, size of the support particles comprised between 1.5 and 5 mm and on which the biofilm
  • the use of rugged high density polyethylene support with the characteristics described above is recommended, or as described in patents FR2707183 and WO9713727 that use a granular plastic support for the treatment of wastewater in biofilm or biofilm biological systems, other than Biological membrane hybrid reactor proposed in our invention.
  • the fraction of support volume in this chamber will be between 15 and 25% v / v, depending on the application.
  • the introduction of the necessary air flow is carried out from the air supply line (8) to a battery of diffusers (9), mounted on a grill, located at the bottom of the draft section.
  • the air flow will be adequate to ensure the transfer of oxygen necessary to produce the biochemical reactions that take place and to maintain the circulation of the plastic support and the mixing liquor in the aerobic chamber.
  • the correct functioning of the hybrid reactor requires that the plastic granular support used be confined in the aerobic chamber (2).
  • a device is placed with which the mixing liquor is separated from the plastic support ( Figures 1 and 4) at the lower end of the firing zone (10 ) attached to the filtration chamber (3).
  • the separation device is formed by a well of rectangular section (10) that has a tube of circular section (11) that communicates the aerobic chamber with a second well (10 ') located in the membrane filtration chamber.
  • the tube used is characterized by having the end located in the well 10 closed and the other end open towards the well 10 'and a longitudinal groove of rectangular section, oriented downwards, through which the mixing liquor passes from 10 to 10' , in this way, the mixing liquor that flows from the aerobic chamber (2) to the filtration chamber (3) is captured, thus avoiding the suction and transport of plastic support particles towards (3).
  • the hearth of the wells (10 and 10 ') of the chambers (2) and (3) are constructed with a slope between 20 and 45 °, in order to minimize sludge deposits in these areas (Section BB', Figure 4).
  • the treated wastewater is separated (as permeate) from the mixing liquor in the chamber (3) using cassettes that have the hollow fiber membrane filtration modules.
  • the cassettes are immersed in the mixing liquor, so that the outer part of the filtration membranes is in contact with the sludge while the inner part of the fibers has been in contact with the filtered effluent that is evacuated, through a conduit connected to a centrifugal pump (13), Figure 1.
  • the use of ultrafiltration or microfiltration modules of hollow fiber membrane made of polysulfones, polypropylene or any other suitable organic polymer is recommended. These modules will be mounted on cassettes or rectangular structures, and with adequate membrane cleaning systems, by means of air current injection, backwashing with permeate or any other system recommended for the application.
  • ZeeWeed ® membrane filtration modules from Zenon Environmental Inc. or equivalent is recommended.
  • a sludge recirculation device ( Figure 1 and Figure 5) formed by a horizontal flow centrifugal impeller (15) will be used.
  • a sludge recirculation device ( Figure 1 and Figure 5) formed by a horizontal flow centrifugal impeller (15) will be used.
  • the sludge is recirculated through this channel by discharging the mixing liquor into the anoxic chamber (1) through a rectangular overflow (17).
  • the size of the reactor depends on both the wastewater flow to be treated and the intrinsic characteristics of the wastewater itself (concentration of pollutants, temperature, presence of inhibitory or toxic substances for biological processes) which are to influence the pollutant loading speed that will be recommended for the reactor design.
  • the organic loading rate is between 2.5 and 7 kg / m 3 -d of COD;
  • the nitrification rate, referred to the aerobic chamber is between 0.5 and 1.5 kg / m 3 -d of N-NH 4 + ;
  • the rate of denitrification, referred to the volume of the anoxic chamber (1) is between 0.5 and 1.2 kg / m 3 -d of
  • the reactor design will consist of three chambers, preferably of rectangular section, or other different geometric shapes combined (oval, circular, etc.).
  • the ratio between the volumes of the three chambers, referred to the total reactor volume, will be 45% for the anoxic chamber (1), 45-50% for the aerobic chamber (2), and 5-10% for the chamber of membrane filtration (3).
  • the hollow fiber membrane filtration modules will have the characteristics and specifications recommended above.
  • the recirculation ratio used would be 3.
  • the concentration of dissolved oxygen in the aerobic chamber would be greater than 3 mg / L, while in the anoxic chamber the oxygen concentration would remain below 0.3 mg / L.
  • the ammonium charge in the Aerated section limits the volume of the system, and is set at 1.0 kg N-NH 4 + / m 3 -d.
  • the organic matter load in the system would be 2.9 kg COD / m 3 -d.
  • the total volume of the reactor would be 14 m 3 , and considering that the percentages of the total volume of the anoxic, aerobic chamber and the membrane compartment are 45%, 45% and 10% of the total volume, they would correspond 6.3 m 3 to the aerobic tank, 6.3 m 3 to the anoxic tank, and the membrane unit compartment a volume of 1.4 m 3 .
  • the system is capable of nitrifying 98% of the ammonium charge that is applied to the system (0.98 kg N-NH + / m 3 -d), nitrogen removal reaches 86%, while COD removal Total in the system (total volume) turns out to be 92% (2.7 kg COD / m 3 -d).

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  • Life Sciences & Earth Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
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  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
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Abstract

The invention relates to a hybrid biological membrane reactor which is used to treat urban and industrial waste water with organic material and nitrogen and which combines micro-organisms in suspension and in a biofilm. The inventive reactor comprises three chambers: an anoxic chamber (1), an air-lift-type aerobic chamber (2) and a filtration chamber (3). The microbial sludge is in suspension in said three chambers, while a rough, granular plastic support is disposed in the aerobic chamber (2). A biofilm is grown on said plastic support with a high fraction of nitrifying micro-organisms and is kept fluidised through the application of an air current which is distributed through diffusers into the chamber. The aforementioned filtration chamber (3) comprises ultrafiltration membrane modules with hollow fibres which are used to separate the treated water from the biological sludge, by recirculating the sludge to the anoxic chamber with the purpose of maintaining a suitable microbial concentration.

Description

TITULO TITLE
Reactor biológico híbrido de membranas para tratamiento de aguas residuales industriales y urbanas.Biological membrane hybrid reactor for industrial and urban wastewater treatment.
DESCRIPCIÓN Reactor biológico híbrido de membranas para tratamiento de aguas residuales industriales y urbanas con materia orgánica y nitrogenada. Está constituido por tres cámaras: anóxica, aerobia y de filtración de membranas. El reactor propuesto es un sistema compacto con el que se consiguen niveles muy bajos o despreciables de sólidos en suspensión en el efluente depurado. Descripción del estado de la técnica de las principales: A) Tecnologías de tratamiento biológico y procesos de eliminación de contaminantes nitrogenados y orgánicos; y B) Sistemas de biorreactores de membranas y reactores híbridos para el tratamiento de aguas residuales.DESCRIPTION Biological membrane hybrid reactor for industrial and urban wastewater treatment with organic and nitrogenous matter. It consists of three chambers: anoxic, aerobic and membrane filtration. The proposed reactor is a compact system with which very low or negligible levels of suspended solids are achieved in the purified effluent. Description of the state of the art of the main ones: A) Biological treatment technologies and processes for the elimination of nitrogen and organic pollutants; and B) Membrane bioreactor systems and hybrid reactors for wastewater treatment.
A) Tecnologías de tratamiento biológico de aguas residuales. Los sistemas de tratamiento biológico se utilizan ampliamente para la eliminación de contaminantes orgánicos, compuestos de nitrógeno y fósforo y se fundamentan en procesos biológicos que emplean cultivos de microorganismos de diferentes especies, fundamentalmente bacterias, hongos, algas, protozoos y metazoos.A) Biological wastewater treatment technologies. Biological treatment systems are widely used for the elimination of organic pollutants, nitrogen and phosphorus compounds and are based on biological processes that employ cultures of microorganisms of different species, mainly bacteria, fungi, algae, protozoa and metazoans.
La eliminación de materia orgánica y nitrogenada, en los sistemas de tratamiento biológico, se lleva a cabo mediante dos clases de microorganismos: microorganismos heterótrofos y bacterias nitrificantes. Los microorganismos heterótrofos se caracterizan por usar compuestos orgánicos en su crecimiento, tanto en condiciones aerobias (usando oxígeno como agente oxidante) o anóxicas (reduciendo nitrito o nitrato a nitrógeno gaseoso). Las bacterias mirificantes oxidan amoníaco a nitrito o nitrato, en condiciones aerobias y se caracterizan por tener menor velocidad de crecimiento y menor tasa de producción celular que las bacterias heterótrofas.The elimination of organic and nitrogenous matter, in biological treatment systems, is carried out by two kinds of microorganisms: heterotrophic microorganisms and nitrifying bacteria. Heterotrophic microorganisms are characterized by using organic compounds in their growth, both in aerobic conditions (using oxygen as an oxidizing agent) or anoxic (reducing nitrite or nitrate to gaseous nitrogen). Mirifying bacteria oxidize ammonia to nitrite or nitrate, under aerobic conditions and are characterized by having a slower growth rate and lower cell production rate than heterotrophic bacteria.
Los procesos tradicionales se clasifican en: (A.l) sistemas de tratamiento de biomasa en suspensión, y (A.2) sistemas de biopelícula. Los primeros se caracterizan porque los microorganismos crecen formando flóculos que se ponen en contacto con el agua residual; y los segundos porque los microorganismos crecen sobre soportes sólidos formando agregados microbianos denominados biopelículas o biofilms (Metcalf & Eddy Inc. Ingeniería de Aguas Residuales, Ed. McGraw HUÍ, (1995); Henze et al. Wastewater treatment, Ed. Springer, (1997)). Los procesos de tratamiento híbrido serían una tercera clase de sistemas que combinan la presencia de biomasa en suspensión y biomasa formando biopelículas. .Traditional processes are classified into: (Al) suspended biomass treatment systems, and (A.2) biofilm systems. The former are characterized in that the microorganisms grow forming flocs that come into contact with the wastewater; and the latter because microorganisms grow on solid supports forming microbial aggregates called biofilms or biofilms (Metcalf & Eddy Inc. Wastewater Engineering, Ed. McGraw HUÍ, (1995); Henze et al. Wastewater treatment, Ed. Springer, (1997 )). Hybrid treatment processes would be a third class of systems that combine the presence of suspended biomass and biomass forming biofilms. .
A.l) En los sistemas de biomasa en suspensión destaca el proceso de lodos activos desarrollado en el Reino Unido en 1914 (Andern E. y Lockett W.T. J. Soc. Chem. Ind. 33, 523 (1914)). Consta de un reactor donde se mantiene un cultivo microbiano en suspensión en condiciones aerobias y un sedimentador para separar el agua residual tratada del lodo microbiano, recirculándolo al sistema biológico. El proceso de lodos activos se diseñó inicialmente para la eliminación de materia orgánica contaminante, pero posteriormente se desarrollaron diferentes configuraciones del proceso para la eliminación de compuestos de nitrógeno y fósforo del agua residual.» Se suelen utilizar configuraciones dotadas de uno o múltiples reactores que se mantienen de forma continua o intermitente en condiciones anóxicas o anaerobias, con la finalidad de promover la eliminación adicional de estos nutrientes. Una de , las limitaciones importantes del sistema es que opera con bajas concentraciones de biomasa, limitando la velocidad de conversión de contaminantes en la unidad, por lo que se deben construir unidades relativamente voluminosas. Aún así, es el proceso de tratamiento biológico más utilizado al ser robusto y fiable.A.l) In the suspended biomass systems the active sludge process developed in the United Kingdom in 1914 stands out (Andern E. and Lockett W.T. J. Soc. Chem. Ind. 33, 523 (1914)). It consists of a reactor where a suspended microbial culture is maintained in aerobic conditions and a settler to separate the treated wastewater from the microbial sludge, recirculating it to the biological system. The active sludge process was initially designed for the elimination of contaminating organic matter, but later different configurations of the process were developed for the elimination of nitrogen and phosphorus compounds from wastewater. »Configurations with one or multiple reactors are usually used. they maintain continuously or intermittently in anoxic or anaerobic conditions, in order to promote the additional elimination of these nutrients. One of the important limitations of the system is that it operates with low biomass concentrations, limiting the speed of conversion of pollutants in the unit, so relatively bulky units must be built. Even so, it is the most widely used biological treatment process because it is robust and reliable.
A.2) En los sistemas de biofilm o biopelícula de microorganismos inmovilizados destacan: 1) filtros percoladores,.2) contactores biológicos rotatorios y 3) filtros biológicos sumergidos. A.2.1) Los filtros percoladores, utilizados desde el siglo XLX, consisten en una columna dotada con un relleno (de guijarros, piedras, listones de madera, soporte plástico, etc.) que se mantiene fijo y sobre el que crece un biofilm formado por microorganismos. En la columna, abierta por sus extremos superior e inferior; el agua residual se esparce a lo largo de todo el sistema poniendo en contacto el agua residual, las biopelículas y el aire. Las principales aplicaciones de los filtros percoladores son la eliminación de materia orgánica y el tratamiento de nitrificación biológica. No se recomienda su utilización cuando se requiera eliminar nitrógeno del agua residual.A.2) In biofilm or biofilm systems of immobilized microorganisms, the following stand out: 1) percolating filters, .2) rotary biological contactors and 3) submerged biological filters. A.2.1) The percolating filters, used since the XLX century, consist of a column equipped with a filling (of pebbles, stones, wooden slats, plastic support, etc.) that remains fixed and on which a formed biofilm grows by microorganisms. In the column, open at its upper and lower ends; wastewater is spread throughout the entire system by contacting wastewater, biofilms and air. The main applications of percolating filters are the elimination of organic matter and the treatment of biological nitrification. Its use is not recommended when it is necessary to remove nitrogen from wastewater.
A.2.2) Los contactores biológicos rotatorios, conocidos como biodiscos, están formados por un soporte de discos plásticos de alta superficie específica sobre los que crece una biopelícula; los discos, acoplados a un eje rotatorio, se hallan sumergidos parcialmente en el agua residual. La rotación de los discos permite la correcta transferencia de oxígeno desde el aire a la biopelícula y facilita el contacto de la biopelícula con los contaminantes presentes en el agua residual. El proceso de biodiscos se originó en la Technical University of Stuttgart (Alemania) en 1955 y la primera planta a escala industrial se puso en marcha en EE. UU. en 1969. Los biodiscos presentan el mismo inconveniente que los filtros percoladores, por lo que se usan poco si hay que eliminar nitrógeno.A.2.2) The rotary biological contactors, known as biodisks, are formed by a support of specific high surface plastic discs on which a biofilm grows; The disks, coupled to a rotating shaft, are partially submerged in the wastewater. The rotation of the discs allows the correct transfer of oxygen from the air to the biofilm and facilitates the contact of the biofilm with the contaminants present in the wastewater. The biodisc process originated at the Technical University of Stuttgart (Germany) in 1955 and the first scale plant industrial was launched in the US UU. in 1969. Biodisks have the same drawback as percolating filters, so they are rarely used if nitrogen needs to be removed.
A.2.3) El principio de operación de los filtros biológicos sumergidos es semejante al de los filtros percoladores, aunque en estos sistemas se inunda totalmente la columna conteniendo el soporte con agua residual. El suministro de aire, si se precisase, se garantiza mediante la inyección de aire y existen también unidades que operan en condiciones anóxicas para la desnitrificación. Los soportes para el crecimiento de las biopelículas son materiales orgánicos como polietileno, poliestireno, poliuretano, partículas granulares de arcilla expandida, partículas de puzolana, arena, u otros materiales con tamaños comprendidos generalmente entre 1 y 5 mm. Los primeros biofiltros a escala industrial fueron desarrollados en los años 70 en Francia usando arcillas expandidas como soporte (Lazarova y Manem, Biofilms II: Process Analysys and Applications, Editor James E. Bryers, (2000)). Algunos de estos sistemas utilizan soportes plásticos granulares, con una densidad ligeramente menor que la del agua, (patentes FR2707183 y WO9713727) sobre los que crece una biopelícula, lo que permite fiuidizar dichos soportes de forma sencilla introduciendo un flujo de gas en el sistema. Los biofiltros sumergidos son unidades muy compactas que se utilizan con diversos fines: eliminación anaerobia, desnitrificación y/o oxidación aerobia de materia orgánica así como nitrifícación de amonio en aguas residuales, y poseen velocidades de eliminación de contaminante relativamente elevadas. Uno de los problemas más generales para su aplicación se deriva de la mayor complejidad - técnica.A.2.3) The principle of operation of submerged biological filters is similar to that of percolating filters, although in these systems the column containing the support with residual water is completely flooded. The air supply, if necessary, is guaranteed by air injection and there are also units that operate under anoxic conditions for denitrification. The supports for the growth of biofilms are organic materials such as polyethylene, polystyrene, polyurethane, granular particles of expanded clay, particles of pozzolana, sand, or other materials with sizes generally between 1 and 5 mm. The first biofilters on an industrial scale were developed in the 70s in France using expanded clays as support (Lazarova and Manem, Biofilms II: Process Analyzes and Applications, Editor James E. Bryers, (2000)). Some of these systems use granular plastic supports, with a density slightly lower than that of water, (patents FR2707183 and WO9713727) on which a biofilm grows, which allows these supports to be easily fiuidized by introducing a gas flow into the system. Submerged biofilters are very compact units that are used for various purposes: anaerobic removal, denitrification and / or aerobic oxidation of organic matter as well as nitrification of ammonia in wastewater, and have relatively high contaminant removal rates. One of the most general problems for its application derives from the greater complexity - technique.
B) Sistemas de biorreactores de membranas y reactores híbridos para el tratamiento de aguas residuales.B) Systems of membrane bioreactors and hybrid reactors for wastewater treatment.
Los sistemas híbridos se caracterizan por combinar la presencia de biomasa en suspensión con biomasa inmovilizada en un soporte en el mismo sistema, lo que permite mantener concentraciones de biocatalizador más elevadas que las que se usan en reactores de biomasa en suspensión, esta peculiaridad constituye una ventaja, ya que se puede depurar el agua residual en equipos híbridos más compactos que los clásicos sistemas de lodos activos. Además, existe la posibilidad de transformar las plantas de lodos activos ya construidas en plantas de sistemas híbridos realizando pequeñas modificaciones en la obra civil y añadiendo un soporte adecuado para aumentar la capacidad de tratamiento de la planta. Los reactores híbridos están adquiriendo cada vez mayor importancia en la depuración de aguas residuales con materia orgánica y nitrógeno, ya que conjugan la robustez de los sistemas de Iodos activos con la mayor capacidad de depuración de los sistemas de biopelículas.Hybrid systems are characterized by combining the presence of suspended biomass with immobilized biomass on a support in the same system, which allows maintaining higher concentrations of biocatalyst than those used in suspended biomass reactors, this peculiarity constitutes an advantage , since it is possible to purify wastewater in more compact hybrid equipment than the classic active sludge systems. In addition, there is the possibility of transforming active sludge plants already built into hybrid system plants by making minor modifications to the civil works and adding adequate support to increase the treatment capacity of the plant. Hybrid reactors are becoming increasingly important in the purification of wastewater with organic matter and nitrogen, as they combine the robustness of active iodine systems with the greater purification capacity of biofilm systems.
Ejemplos de sistemas híbridos son la patente US5061368 y las referencias bibliográficas (Andreottola et al.; Münch et al.; Θdegaard et al.; Wat. Sci. Technol. v41, n° 4-5, (1999)) que utilizan soportes plásticos como los descritos en las patentes US5458779, US5543039 y US6126829 para mejorar el rendimiento de diversos reactores biológicos en las que crece biomasa tanto en suspensión como en biofilms.Examples of hybrid systems are US5061368 and bibliographic references (Andreottola et al .; Münch et al .; Θdegaard et al .; Wat. Sci. Technol. V41, No. 4-5, (1999)) using plastic supports such as those described in patents US5458779, US5543039 and US6126829 to improve the performance of various biological reactors in which biomass grows both in suspension and in biofilms.
La patente US5061368 emplea un sistema híbrido que alterna cámaras anaerobias y. anóxicas, manteniendo biomasa en suspensión en todo el sistema y biomasa inmovilizada en cubitos de un gel retenidas en cámaras aerobias nitrificantes. Una desventaja de este sistema es que inmoviliza de forma artificial microorganismos nitrificantes en cubitos de gel de polietilenglicol que hay que reponer periódicamente para suplir aquellas partículas de gel que se rompen o desgastan, por lo que es preciso fabricar nuevos cubitos de gel, no solo durante la etapa de puesta en marcha, sino también durante la operación en continuo del sistema. Además, no se pueden aplicar velocidades de carga muy elevadas ya que pueden causar la ruptura de los cubitos de gel por el aumento de la velocidad de crecimiento de los microorganismos inmovilizados.US5061368 uses a hybrid system that alternates anaerobic and chambers. anoxic, maintaining suspended biomass throughout the system and immobilized biomass in a gel cubes retained in nitrifying aerobic chambers. A disadvantage of this system is that it artificially immobilizes nitrifying microorganisms in polyethylene glycol gel cubes that must be periodically replenished to replace those gel particles that break or wear out, so it is necessary to manufacture new gel cubes, not only during the commissioning stage, but also during the continuous operation of the system. In addition, very high loading rates cannot be applied since they can cause the breakage of the gel cubes by increasing the growth rate of the immobilized microorganisms.
Otro inconveniente de los sistemas descritos en las publicaciones mencionadas anteriormente, son los que pueden surgir de la aplicación de velocidades de carga orgánica elevadas, así como de las propias características físico-químicas del agua residual, que pueden afectar negativamente a las propiedades de sedimentabilidad del fango que se genera en los sistemas biológicos y por tanto puede afectar negativamente a la separación, mediante sedimentadores, de sólidos del agua tratada. Los sistemas híbridos mencionados utilizan sedimentadores por lo que, para determinadas aplicaciones y en determinadas condiciones, su eficiencia se puede ver afectada por una incorrecta separación de los sólidos del agua tratada.Another drawback of the systems described in the publications mentioned above, are those that may arise from the application of high organic loading rates, as well as from the physical-chemical characteristics of the wastewater itself, which may adversely affect the sedimentability properties of the sludge that is generated in biological systems and therefore can negatively affect the separation, by sedimentators, of solids from treated water. The hybrid systems mentioned use sedimentators so, for certain applications and under certain conditions, their efficiency can be affected by an incorrect separation of solids from treated water.
La primera cita sobre la utilización de sistemas de membrana data de 1969. Se utilizó una membrana de ultrafiltración para la separación del agua residual tratada de la biomasa en un sistema de lodos activos. La combinación de las dos tecnologías ha llevado al desarrollo de tres grupos de procesos biológicos de membranas: i) separación líquido- sólido mediante membranas para la retención de la biomasa en reactores biológicos; ii) utilización de membranas permeables a un compuesto gaseoso para la transferencia de oxígeno sin burbujeo en reactores; iii) proceso de membranas extractivo aplicado para la eliminación de compuestos orgánicos degradables en aguas residuales industriales problemáticas (Brindle K. and Stephenson T., Biotechnol. Bioeng. 49, 601-610, (1996)). Destacar que el sistema híbrido de membranas propuesto en nuestra invención es una aplicación novedosa más del primer grupo (i), donde se utilizan sistemas de filtración de membranas para la separación del agua residual de los microorganismos.The first quotation on the use of membrane systems dates from 1969. An ultrafiltration membrane was used for the separation of treated wastewater from biomass in an active sludge system. The combination of the two technologies has led to the development of three groups of biological membrane processes: i) liquid separation solid by membranes for the retention of biomass in biological reactors; ii) use of permeable membranes to a gaseous compound for oxygen transfer without bubbling in reactors; iii) extractive membrane process applied for the elimination of degradable organic compounds in problematic industrial wastewater (Brindle K. and Stephenson T., Biotechnol. Bioeng. 49, 601-610, (1996)). Note that the hybrid membrane system proposed in our invention is a novel application of the first group (i), where membrane filtration systems are used for the separation of residual water from microorganisms.
La mayor parte de los sistemas de tratamiento biológico que utilizan membranas en la actualidad, son modificaciones del proceso de lodos activos, donde se ha sustituido el sedimentador secundario, empleado en los procesos tradicionales, por unidades de filtración de membranas para la separación de los microorganismos en suspensión del agua tratada en reactores de biomasa en suspensión. Las membranas que se han utilizado para este fin son membranas de microfiltración o ultrafiltración fabricadas con materiales orgánicos o inorgánicos dispuestos en módulos de fibras huecas, de placas o tubulares que se pueden colocar dentro o fuera del reactor biológico (Günder B. and Krauth K., Wat. Sci.Most of the biological treatment systems that use membranes today are modifications of the active sludge process, where the secondary settler, used in traditional processes, has been replaced by membrane filtration units for the separation of microorganisms in suspension of treated water in suspended biomass reactors. The membranes that have been used for this purpose are microfiltration or ultrafiltration membranes made of organic or inorganic materials arranged in hollow fiber, plate or tubular modules that can be placed inside or outside the biological reactor (Günder B. and Krauth K. , Wat. Sci.
Technol., vol 38, pp 382-393 (1998); Buisson H. et al. Wat. Sci. Technol. 37(9), pp. 89-95Technol., Vol 38, pp 382-393 (1998); Buisson H. et al. Wat. Sci. Technol. 37 (9), pp. 89-95
(1998); Günder B. and Krauth K., Wat. Sci. Technol., vól 40, pp 311-320 (1999), Ghyoot(1998); Günder B. and Krauth K., Wat. Sci. Technol., Vol 40, pp 311-320 (1999), Ghyoot
W. and Nerstraete W., Wat. Res., 34, pp. 205-215, (2000)). Asimismo, existen diversas patentes que se basan en la utilización de diferentes módulos de filtración de membranas que se pueden o podrían usar en la separación del agua residual tratada en biorreactores de biomasa en suspensión (patentes US5558774 y US6303035).W. and Nerstraete W., Wat. Res., 34, pp. 205-215, (2000)). Likewise, there are several patents that are based on the use of different membrane filtration modules that can or could be used in the separation of wastewater treated in suspended biomass bioreactors (US5558774 and US6303035).
La presente invención supone mejoras en los sistemas para el tratamiento biológico de aguas residuales, en general, y reactores híbridos, en particular. Una de las principales características del reactor híbrido propuesto es la de confinar partículas de un soporte granular plástico en la cámara aerobia, con densidad ligeramente menor a la del agua. Este soporte no rompe ni se deteriora por el uso en el sistema; además no va a romper por crecimiento de la biomasa en el mismo (como puede ocurrir en sistemas que utilizan microorganismos inmovilizados en el seno de geles poliméricos) ya que el crecimiento se limita a la superficie del soporte plástico. De esta forma se ahorra también la necesidad de disponer de un stock de partículas de gel con microorganismos.The present invention involves improvements in systems for the biological treatment of wastewater, in general, and hybrid reactors, in particular. One of the main characteristics of the proposed hybrid reactor is to confine particles of a plastic granular support in the aerobic chamber, with a slightly lower density than that of water. This support does not break or deteriorate due to use in the system; In addition, it will not break due to the growth of the biomass in it (as can occur in systems that use immobilized microorganisms within polymer gels) since growth is limited to the surface of the plastic support. This also saves the need for a stock of gel particles with microorganisms.
Otra ventaja es la utilización de un sistema de filtración de membranas de fibras huecas. Como se mencionó, en los sistemas híbridos que utilizan sedimentadores para separar el agua depurada del lodo biológico, la eficiencia de la separación depende de las propiedades de sedimentabilidad del lodo, y puede empeorar si se aplican cargas contaminantes elevadas en el sistema. El sistema de filtración de membrana propuesto independiza el proceso de separación del agua residual tratada y el lodo de las propiedades de sedimentabilidad, por lo que se pueden aplicar velocidades de carga más elevadas sin riesgo de sufrir problemas de operación del sistema. Además, se evita el posible lavado del fango del reactor biológico.Another advantage is the use of a filtration system of hollow fiber membranes. As mentioned, in hybrid systems that use settlers to separating the purified water from the biological sludge, the separation efficiency depends on the sedimentability properties of the sludge, and can worsen if high pollutant loads are applied in the system. The proposed membrane filtration system makes the process of separating treated wastewater and sludge independent of sedimentability properties, so that higher loading speeds can be applied without risk of system operation problems. In addition, the possible washing of the sludge from the biological reactor is avoided.
La instalación de unidades de filtración de membrana en el reactor híbrido hace posible la obtención de un efluente con niveles bajos de sólidos en suspensión, que cumpliría los requerimientos de vertidos más exigentes de este contaminante, disminuye notablemente el vertido de microorganismos con el efluente (incluidos patógenos y otros vectores sanitarios); además, es apropiado para vertidos en las proximidades de zonas de cultivos marinos o piscifactorías y de zonas de captación de aguas utilizadas para el riego o la producción de agua potable. En el reactor biológico propuesto se confina el soporte granular plástico con las biopelículas en la cámara aerobia, usando dispositivos de separación que permiten el paso libre del licor de mezcla, con los microorganismos en suspensión entre las tres cámaras de las que consta la unidad.The installation of membrane filtration units in the hybrid reactor makes it possible to obtain an effluent with low levels of suspended solids, which would meet the most demanding discharge requirements of this contaminant, significantly decreases the discharge of microorganisms with the effluent (including pathogens and other health vectors); In addition, it is suitable for discharges in the vicinity of areas of marine culture or fish farms and areas of water catchment used for irrigation or the production of drinking water. In the proposed biological reactor the plastic granular support is confined with the biofilms in the aerobic chamber, using separation devices that allow the free passage of the mixing liquor, with the microorganisms in suspension between the three chambers of which the unit consists.
Con esta propuesta es posible operar el sistema con un lodo en suspensión que contiene una fracción elevada de microorganismos heterótrofos precisados para desnitrificar en la cámara anóxica y eliminar restos de materia orgánica soluble que pudiesen llegar a la cámara aerobia; así se limita el crecimiento de bacterias heterótrofas en el biofilm, se incentiva el crecimiento de bacterias nitrificantes en el biofilm y por ello se evita que se inhiba o reduzca la capacidad mirificante de la biopelícula que crece sobre el soporte plástico. Todo esto permite que se pueda aplicar y operar con velocidades de cargas orgánicas (kg DQO/m3-d) y nitrogenadas (kg N-NH4 +/m3-d) relativamente elevadas y mayores que la de sistemas anteriormente mencionados, sin que se sufran por ello disminuciones de eficiencia de depuración o problemas debidos a la ruptura o colmatación del soporte por el crecimiento de la biomasa. Las figuras 1-5 representan el reactor biológico híbrido de membranas:With this proposal it is possible to operate the system with a sludge in suspension that contains a high fraction of heterotrophic microorganisms required to denitrify in the anoxic chamber and eliminate remains of soluble organic matter that could reach the aerobic chamber; thus, the growth of heterotrophic bacteria in the biofilm is limited, the growth of nitrifying bacteria in the biofilm is encouraged and, therefore, it is prevented that the mirifying capacity of the biofilm growing on the plastic support is inhibited or reduced. All this allows it to be applied and operated with speeds of organic loads (kg COD / m 3 -d) and nitrogenous (kg N-NH 4 + / m 3 -d) relatively high and higher than the systems mentioned above, without that there is a decrease in efficiency of purification or problems due to the rupture or clogging of the support due to the growth of biomass. Figures 1-5 represent the hybrid biological membrane reactor:
Figura 1. Esquema del reactor constituido por las tres cámaras: cámara anóxica (1), cámara aerobia (2), y cámara de filtración (3). Figura 2. Perspectiva tridimensional del reactor, mostrando las tres cámaras, las dos placas deflectoras (7) de la cámara aerobia, canal de recirculación del agua residual (18) y rebosadero (17). Se ha destacado la obra civil, omitiendo equipos auxiliares.Figure 1. Diagram of the reactor consisting of the three chambers: anoxic chamber (1), aerobic chamber (2), and filtration chamber (3). Figure 2. Three-dimensional perspective of the reactor, showing the three chambers, the two baffle plates (7) of the aerobic chamber, wastewater recirculation channel (18) and overflow (17). The civil work has been highlighted, omitting auxiliary equipment.
Figura 3. Forma y disposición de la conducción de paso del licor de mezcla (6) desde la cámara anóxica (1) a la cámara aerobia (2).Figure 3. Shape and arrangement of the passage of the mixing liquor (6) from the anoxic chamber (1) to the aerobic chamber (2).
Figura 4. Pozos de captación (10 y 10') del licor de mezcla de la cámara aerobia (2) a la cámara de filtración (3). La conducción (11) se utiliza para el transporte del agua residual entre las cámaras.Figure 4. Collection wells (10 and 10 ') of the mixing liquor from the aerobic chamber (2) to the filtration chamber (3). The conduit (11) is used for the transport of wastewater between the chambers.
Figura 5. Sección AA' (en figura 1) que muestra un dispositivo de impulsión del licor de mezcla desde la cámara de filtración a la cámara anóxica, mostrando el agitador centrífugo (15), la conducción (16) y el canal de recirculación (18).Figure 5. Section AA '(in figure 1) showing a mixing liquor delivery device from the filtration chamber to the anoxic chamber, showing the centrifugal stirrer (15), the conduit (16) and the recirculation channel ( 18).
Las figuras 1 y 2 representan las características esenciales del sistema. Consta de tres cámaras: cámara anóxica (1); cámara aerobia, tipo air-lift (2); y cámara de filtración (3). En las tres cámaras se mantiene el lodo microbiano ' en suspensión. En la cámara aerobia (2) se confina, además, un soporte plástico granular y rugoso de densidad inferior a la del agua, sobre el que crece una biopelícula con una fracción elevada de microorganismos nitrificantes. El sistema incorpora en su cámara de filtración (3) módulos de membranas de ultrafiltración de fibras huecas (12) que se utilizan para separar el agua tratada del lodo biológico, recirculando el lodo de esta cámara a la anóxica (1).Figures 1 and 2 represent the essential characteristics of the system. It consists of three cameras: anoxic chamber (1); aerobic camera, air lift type (2); and filtration chamber (3). In the three chambers microbial sludge is maintained 'suspension. In the aerobic chamber (2), a granular and rough plastic support of lower density than water is confined, on which a biofilm with a high fraction of nitrifying microorganisms grows. The system incorporates in its filtration chamber (3) modules of ultrafiltration membranes of hollow fibers (12) that are used to separate the treated water from the biological sludge, recirculating the sludge of this chamber to the anoxic (1).
La figura 1 muestra como se introduce el agua residual en la cámara anóxica (1) a través de la conducción ubicada en la parte superior de la misma (4) mezclándose el influente con el licor de mezcla presente en la cámara. La homogeneidad de la mezcla formada por microorganismos en suspensión y agua residual se garantiza utilizando un dispositivo adecuado de agitación mecánica (5), como un acelerador de flujo o agitador mecánico.Figure 1 shows how the wastewater is introduced into the anoxic chamber (1) through the conduit located in the upper part thereof (4), the influent being mixed with the mixing liquor present in the chamber. The homogeneity of the mixture formed by microorganisms in suspension and residual water is guaranteed using a suitable mechanical agitation device (5), such as a flow accelerator or mechanical agitator.
En la cámara (1) se produce la desnitrificación biológica por la que parte de los aniones de nitrógeno presentes en el agua se reducen a nitrógeno gaseoso, mediante el biocatalizador presente, efectuándose además, la eliminación de una fracción elevada de los contaminantes orgánicos en la' reacción de desnitrificación y la adsorción de compuestos orgánicos solubles, de forma que se consigue eliminar parte de la materia orgánica del agua que de otra forma, podría ser asimilada por las biopelículas presentes en la cámara aerobia (2). La conducción de la figura 3 permite el paso del licor de mezcla desde la cámara anóxica (1) a la aerobia (2). Esta vía de paso está formado por una o más conducciones de sección circular (6) por las que circula el licor de mezcla procedente de (1) hacia (2). El diseño de la conducción en ángulo se plantea de forma que se limite la retromezcla del fluido entre las cámaras y minimice o impida tanto la entrada de soporte de la cámara aerobia (2) a la cámara anóxica (1) como la deposición de lodo en el mismo. La inclinación del tramo inclinado del tubo con respecto al tramo horizontal del mismo estará comprendida entre 20° y 90°.In the chamber (1) the biological denitrification takes place whereby part of the nitrogen anions present in the water are reduced to gaseous nitrogen, by means of the biocatalyst present, also eliminating a high fraction of the organic pollutants in the Denitrification reaction and adsorption of soluble organic compounds, so that part of the organic matter can be removed from the water that could otherwise be assimilated by the biofilms present in the aerobic chamber (2). The conduction of figure 3 allows the mixing liquor to pass from the anoxic chamber (1) to the aerobic (2). This passageway is formed by one or more circular section ducts (6) through which the mixing liquor from (1) to (2) circulates. The design of the conduction at an angle is set in such a way that the back-mixing of the fluid between the chambers is limited and minimizes or prevents both the support entrance of the aerobic chamber (2) to the anoxic chamber (1) and the deposition of mud in the same. The inclination of the inclined section of the tube with respect to the horizontal section thereof will be between 20 ° and 90 °.
La cámara aerobia (2) es un dispositivo tipo air-lift en el que se instalan dos placas deflectoras o bailes que dividen esta cámara en tres secciones rectangulares (figuras 1 y 2): una sección central denominada riser o tiro, que dispone en su parte inferior de difusores por los que se distribuye aire, y dos secciones en los laterales denominadas bajantes o down-comers. En esta cámara aerobia (2) se confina un soporte granular rugoso de plástico con una densidad del 5 % al 15 % menor que la del agua, tamaño de las partículas de soporte comprendido entre 1,5 y 5 mm y sobre las cuales crece la biopelícula. Se recomienda la utilización de soporte rugoso de polietileno de alta densidad con las características descritas anteriormente, o como las descritas en las patentes FR2707183 y WO9713727 que utilizan un soporte plástico granular para el tratamiento de aguas residuales en sistemas biológicos de biofilm o biopelícula, diferentes al reactor biológico híbrido de membrana que se propone en nuestra invención. La fracción de volumen de soporte en esta cámara estará comprendida entre el 15 y el 25 % v/v, según aplicación.The aerobic camera (2) is an air-lift type device in which two deflector plates or dances are installed that divide this camera into three rectangular sections (figures 1 and 2): a central section called riser or shot, which has in its lower part of diffusers through which air is distributed, and two sections on the sides called downspouts or down-comers. In this aerobic chamber (2) a rough granular plastic support is confined with a density of 5% to 15% less than that of water, size of the support particles comprised between 1.5 and 5 mm and on which the biofilm The use of rugged high density polyethylene support with the characteristics described above is recommended, or as described in patents FR2707183 and WO9713727 that use a granular plastic support for the treatment of wastewater in biofilm or biofilm biological systems, other than Biological membrane hybrid reactor proposed in our invention. The fraction of support volume in this chamber will be between 15 and 25% v / v, depending on the application.
En la cámara aerobia la introducción del flujo de aire necesario se realiza desde la conducción de suministro de aire (8) hacia una batería de difusores (9), montados en parrilla, ubicada en la parte inferior de la sección de tiro. El flujo de aire será el adecuado para asegurar la transferencia del oxígeno necesario para que se produzcan las reacciones bioquímicas que tienen lugar y para mantener la circulación del soporte plástico y el licor de mezcla en la cámara aerobia.In the aerobic chamber the introduction of the necessary air flow is carried out from the air supply line (8) to a battery of diffusers (9), mounted on a grill, located at the bottom of the draft section. The air flow will be adequate to ensure the transfer of oxygen necessary to produce the biochemical reactions that take place and to maintain the circulation of the plastic support and the mixing liquor in the aerobic chamber.
El correcto funcionamiento del reactor híbrido exige que el soporte granular plástico utilizado quede confinado en la cámara aerobia (2). Para evitar salidas del soporte granular plástico hacia la cámara de filtración (3) se coloca un dispositivo con el que se realiza la separación del licor de mezcla del soporte plástico (Figuras 1 y 4) en el extremo inferior de la zona de tiro (10) anexa a la cámara de filtración (3). El dispositivo de separación está formado por un pozo de sección rectangular (10) que dispone de un tubo de sección circular (11) que comunica la cámara aerobia con un segundo pozo (10') ubicado en la cámara de filtración de membranas. El tubo utilizado se caracteriza por tener el extremo situado en el pozo 10 cerrado y el otro extremo abierto hacia el pozo 10' y una ranura longitudinal de sección rectangular, orientada hacia abajo, por la que pasa el licor de mezcla de 10 hacia 10', de esta forma se capta el licor de mezcla que fluye desde la cámara aerobia (2) a la cámara de filtración (3), evitando así la succión y transporte de partículas plásticas de soporte hacia (3). La solera de los pozos (10 y 10') de las cámaras (2) y (3) se construyen con una pendiente comprendida entre 20 y 45°, con objeto de minimizar los depósitos de lodos en estas zonas (Sección BB', Figura 4).The correct functioning of the hybrid reactor requires that the plastic granular support used be confined in the aerobic chamber (2). To avoid exits of the plastic granular support towards the filtration chamber (3) a device is placed with which the mixing liquor is separated from the plastic support (Figures 1 and 4) at the lower end of the firing zone (10 ) attached to the filtration chamber (3). The separation device is formed by a well of rectangular section (10) that has a tube of circular section (11) that communicates the aerobic chamber with a second well (10 ') located in the membrane filtration chamber. The tube used is characterized by having the end located in the well 10 closed and the other end open towards the well 10 'and a longitudinal groove of rectangular section, oriented downwards, through which the mixing liquor passes from 10 to 10' , in this way, the mixing liquor that flows from the aerobic chamber (2) to the filtration chamber (3) is captured, thus avoiding the suction and transport of plastic support particles towards (3). The hearth of the wells (10 and 10 ') of the chambers (2) and (3) are constructed with a slope between 20 and 45 °, in order to minimize sludge deposits in these areas (Section BB', Figure 4).
El agua residual tratada se separa (como permeado) del licor de mezcla en la cámara (3) utilizando unos casetes que disponen de los módulos de filtración de membrana de fibras huecas. Los casetes se sumergen en el seno del licor de mezcla, de forma que la parte externa de las membranas de filtración se encuentren en contacto con el lodo mientras que la parte interna de las fibras se haya en contacto con el efluente filtrado que se evacúa, a través de una conducción conectada a una bomba centrífuga (13), Figura 1. Se recomienda la utilización de módulos de ultrafiltración o microfiltración de membrana de fibra hueca fabricados en polisulfonas, polipropileno o cualquier otro polímero orgánico adecuado. Dichos módulos irán montados en casetes o estructuras rectangulares, y con sistemas de limpieza de la membrana adecuados, mediante inyección de corriente de aire, retro lavado con el permeado o cualquier otro sistema recomendado para la aplicación. Se recomienda el uso de módulos de filtración de membranas ZeeWeed® de la casa Zenon Environmental Inc. o equivalentes.The treated wastewater is separated (as permeate) from the mixing liquor in the chamber (3) using cassettes that have the hollow fiber membrane filtration modules. The cassettes are immersed in the mixing liquor, so that the outer part of the filtration membranes is in contact with the sludge while the inner part of the fibers has been in contact with the filtered effluent that is evacuated, through a conduit connected to a centrifugal pump (13), Figure 1. The use of ultrafiltration or microfiltration modules of hollow fiber membrane made of polysulfones, polypropylene or any other suitable organic polymer is recommended. These modules will be mounted on cassettes or rectangular structures, and with adequate membrane cleaning systems, by means of air current injection, backwashing with permeate or any other system recommended for the application. The use of ZeeWeed ® membrane filtration modules from Zenon Environmental Inc. or equivalent is recommended.
En la cámara de filtración (3) se purga de forma controlada el exceso de lodos que se genera a través de una conducción que parte de la cámara de filtración (3) y se acopla a la bomba (14), Figura 1.In the filtration chamber (3), excess sludge that is generated through a conduit that starts from the filtration chamber (3) and is coupled to the pump (14) is purged in a controlled manner, Figure 1.
Para la recirculación del lodo retenido en la cámara de filtración (3) hacia la cámara anóxica (1) se procederá a utilizar un dispositivo de recirculación de fangos (figura 1 y figura 5) formado por un impulsor centrífugo de flujo horizontal (15) que dirige a través de la conducción (16) una corriente de licor de mezcla desde la cámara de filtración (3) a un canal de recirculación (18) ubicado en un lateral del sistema (figura 2 y figura 5). El lodo se recircula a través de este canal descargando el licor de mezcla en la cámara anóxica (1) a través de un rebosadero rectangular (17). De acuerdo con la presente invención, el tamaño del reactor depende tanto del caudal de agua residual a tratar como de las características intrínsecas del propia agua residual (concentración de contaminantes, temperatura, presencia de sustancias inhibidoras o tóxicas para los procesos biológicos) las cuales van a incidir en la velocidad de carga de contaminante que se recomendará para el diseño del reactor.For the recirculation of the sludge retained in the filtration chamber (3) towards the anoxic chamber (1), a sludge recirculation device (Figure 1 and Figure 5) formed by a horizontal flow centrifugal impeller (15) will be used. directs through the conduit (16) a stream of mixing liquor from the filtration chamber (3) to a recirculation channel (18) located on one side of the system (figure 2 and figure 5). The sludge is recirculated through this channel by discharging the mixing liquor into the anoxic chamber (1) through a rectangular overflow (17). In accordance with the present invention, the size of the reactor depends on both the wastewater flow to be treated and the intrinsic characteristics of the wastewater itself (concentration of pollutants, temperature, presence of inhibitory or toxic substances for biological processes) which are to influence the pollutant loading speed that will be recommended for the reactor design.
Para el caso de aguas residuales urbanas e industriales con componentes orgánicos fácilmente biodegradables, la velocidad de carga orgánica está comprendida entre 2,5 y 7 kg/m3-d de DQO; la velocidad de nitrificación, referida a la cámara aerobia, está comprendida entre 0,5 y 1,5 kg/m3-d de N-NH4 +; y la velocidad de desnitrificación, referido al volumen de la cámara anóxica (1), está comprendida entre 0,5 y 1,2 kg/m3-d deIn the case of urban and industrial wastewater with easily biodegradable organic components, the organic loading rate is between 2.5 and 7 kg / m 3 -d of COD; the nitrification rate, referred to the aerobic chamber, is between 0.5 and 1.5 kg / m 3 -d of N-NH 4 + ; and the rate of denitrification, referred to the volume of the anoxic chamber (1), is between 0.5 and 1.2 kg / m 3 -d of
El diseño del reactor estará formado por tres cámaras, preferentemente de sección rectangular, u otras formas geométricas diferentes combinadas (ovalado, circular, etc.). La relación entre los volúmenes de las tres cámaras, referido al volumen total del reactor, será del 45 % para la cámara anóxica (1), 45 - 50 % para la cámara aerobia (2), y 5 - 10 % para la cámara de filtración de membranas (3).The reactor design will consist of three chambers, preferably of rectangular section, or other different geometric shapes combined (oval, circular, etc.). The ratio between the volumes of the three chambers, referred to the total reactor volume, will be 45% for the anoxic chamber (1), 45-50% for the aerobic chamber (2), and 5-10% for the chamber of membrane filtration (3).
Los módulos de filtración de membrana de fibra hueca tendrán las características y especificaciones recomendadas anteriormente.The hollow fiber membrane filtration modules will have the characteristics and specifications recommended above.
Para el cálculo de la superficie del módulo de membranas que se precisa, es necesario contactar con el proveedor o fabricante de dicho módulo. Como orientación indicar que los módulos recomendados tienen una capacidad para filtrar, en condiciones de operación estacionarias, entre 20 y 30 L de efluente permeado por metro cuadrado de membrana y hora de operación.To calculate the surface area of the membrane module required, it is necessary to contact the supplier or manufacturer of that module. As a guideline, indicate that the recommended modules have a capacity to filter, under stationary operating conditions, between 20 and 30 L of effluent permeated per square meter of membrane and hour of operation.
EJEMPLO DE UNA REALIZACIÓNEXAMPLE OF AN EMBODIMENT
Reactor biológico híbrido de membranas para el tratamiento de aguas residuales de industrias de conservas de pescado.Biological membrane hybrid reactor for the treatment of wastewater from canned fish industries.
Caudal de agua residual afluente 21 m3/h; concentración de DQO total medida a la entrada del sistema 1900 mgl /L, concentración de amonio 300 mg N-NH +/L.Flow of residual water tributary 21 m 3 / h; Total COD concentration measured at system input 1900 mg l / L, ammonium concentration 300 mg N-NH + / L.
La relación de recirculación utilizada sería de 3. La concentración de oxígeno disuelto en la cámara aerobia sería superior a 3 mg/L, mientras que en la cámara anóxica la concentración de oxígeno se mantendría por debajo de 0,3 mg/L. La carga de amonio en la sección aireada limita el volumen del sistema, y se establece en 1,0 kg N-NH4 +/m3-d. La carga de materia orgánica en el sistema sería de 2,9 kg DQO/m3-d. El volumen total del reactor sería de 14 m3, y considerando que los porcentajes del volumen total de la cámara anóxica, aerobia y del compartimento de membrana son de 45 %, 45 % y 10 % del volumen total, corresponderían 6,3 m3 al tanque aerobio, 6,3 m3 al tanque anóxico, y el compartimento de la unidad de membrana un volumen de 1,4 m3. Se precisa un volumen de 1,26 m3 (20 % v/v) de soporte granular plástico, con las características previamente indicadas, para promover el crecimiento de biopelículas nitrificantes en la cámara aerobia.The recirculation ratio used would be 3. The concentration of dissolved oxygen in the aerobic chamber would be greater than 3 mg / L, while in the anoxic chamber the oxygen concentration would remain below 0.3 mg / L. The ammonium charge in the Aerated section limits the volume of the system, and is set at 1.0 kg N-NH 4 + / m 3 -d. The organic matter load in the system would be 2.9 kg COD / m 3 -d. The total volume of the reactor would be 14 m 3 , and considering that the percentages of the total volume of the anoxic, aerobic chamber and the membrane compartment are 45%, 45% and 10% of the total volume, they would correspond 6.3 m 3 to the aerobic tank, 6.3 m 3 to the anoxic tank, and the membrane unit compartment a volume of 1.4 m 3 . A volume of 1.26 m 3 (20% v / v) of plastic granular support, with the previously indicated characteristics, is required to promote the growth of nitrifying biofilms in the aerobic chamber.
El sistema es capaz de nitrificar el 98 % de la carga de amonio que se aplica al sistema (0,98 kg N-NH +/m3-d), la eliminación de nitrógeno alcanza 86 %, mientras que la eliminación de la DQO total en el sistema (volumen total) resulta ser el 92 % (2,7 kg DQO/m3-d). The system is capable of nitrifying 98% of the ammonium charge that is applied to the system (0.98 kg N-NH + / m 3 -d), nitrogen removal reaches 86%, while COD removal Total in the system (total volume) turns out to be 92% (2.7 kg COD / m 3 -d).

Claims

REIVINDICACIONES
1.- Reactor biológico híbrido de membranas para tratamiento de aguas residuales industriales y urbanas, caracterizado por estar compuesto de tres cámaras: cámara anóxica (1), cámara aerobia (2) y cámara de filtración de membranas (3); las cámaras son de sección rectangular o cualquier otra forma geométrica. El reactor es de aplicación en depuración de materia orgánica y nitrogenada, y eliminación de sólidos en suspensión.1.- Hybrid biological membrane reactor for industrial and urban wastewater treatment, characterized by being composed of three chambers: anoxic chamber (1), aerobic chamber (2) and membrane filtration chamber (3); The cameras are of rectangular section or any other geometric shape. The reactor is applicable in the purification of organic and nitrogenous matter, and removal of suspended solids.
2.- Reactor, según la reivindicación 1, caracterizado porque la cámara anóxica (1) está dotada de uno o varios agitadores mecánicos, un rebosadero de sección rectangular en uno de sus laterales. Sobre la cámara se descarga un agua residual influente a, través de una conducción ubicada en la parte superior de la cámara. En la cámara anóxica se pone en contacto el agua residual influente con el licor de mezcla y una corriente de lodo recirculado desde la cámara de filtración de membranas (3), eliminándose nitrato y una fracción de la materia orgánica presente. Se garantizará la homogeneidad del licor de mezcla y se evitará la deposición de fangos en el fondo con la utilización de los agitadores mecánicos adecuados.2. Reactor according to claim 1, characterized in that the anoxic chamber (1) is provided with one or more mechanical stirrers, an overflow of rectangular section on one of its sides. An influent wastewater is discharged onto the chamber through a conduit located in the upper part of the chamber. In the anoxic chamber the influent residual water is contacted with the mixing liquor and a stream of recirculated sludge from the membrane filtration chamber (3), eliminating nitrate and a fraction of the organic matter present. The homogeneity of the mixing liquor will be guaranteed and sludge deposition at the bottom will be avoided with the use of suitable mechanical stirrers.
3.- Reactor, según las reivindicaciones 1 y 2, caracterizado por conducto(s) angular(es) de sección circular(es) que comunica(n) la cámara anóxica (1) con la cámara aerobia (2). El conducto tiene la forma de tubo en ángulo con dos tramos: uno horizontal y otro con una inclinación comprendida entre 20 y 90° respecto al primer tramo.3. Reactor according to claims 1 and 2, characterized by angular duct (s) of circular section (s) that communicates the anoxic chamber (1) with the aerobic chamber (2). The duct has the shape of an angled tube with two sections: one horizontal and the other with an inclination between 20 and 90 ° with respect to the first section.
4.- Reactor, según la reivindicación 1, caracterizado porque la cámara aerobia (2) de tipo airlift, dispondrá .de un soporte granular plástico para el crecimiento de biopelículas. La cámara está dotada de dos placas deflectoras o bailes, que dividen la cámara en tres secciones, la sección central aireada y las otras dos secciones laterales no aireadas, que se comunican entre sí tanto a través de la parte inferior como superior de la cámara. En la parte inferior de la sección aireada se dispondrá una parrilla de difusores. En la cámara aerobia se suministra una corriente de aire a través de la parrilla de difusores, para homogeneizar el licor de mezcla y las partículas de soporte granular plástico y para transferir el oxígeno que se precisa en las reacciones bioquímicas que tienen lugar, oxidación de materia orgánica y reacción de nulificación biológica. La corriente de aire induce la circulación del soporte y el licor de mezcla desde la sección central aireada, en sentido ascendente, y las dos secciones laterales, en sentido descendente.4. Reactor according to claim 1, characterized in that the aerobic chamber (2) of the airlift type will have a plastic granular support for the growth of biofilms. The chamber is equipped with two deflector plates or dances, which divide the chamber into three sections, the aerated central section and the other two non-aerated side sections, which communicate with each other both through the lower and upper part of the chamber. At the bottom of the aerated section a diffuser grill will be arranged. An air stream is supplied in the aerobic chamber through the diffuser grill, to homogenize the mixing liquor and the particles of plastic granular support and to transfer the oxygen that is required in the biochemical reactions that take place, oxidation of matter Organic and biological nullification reaction. Air flow induces the circulation of the support and the mixing liquor from the aerated central section, in the upward direction, and the two lateral sections, in the downward direction.
5.- Reactor, según las reivindicaciones 1 y 4, caracterizado por un soporte granular rugoso de plástico de polietileno de alta densidad o material plástico con características equivalentes-, con una densidad del 5 al 15 % menor que la del agua, tamaño comprendido entre 1,5 y 5 mm. El volumen del soporte, ubicado en la cámara aerobia, estará comprendido entre el 15 y el 25 % v/v, referido al volumen de la cámara aerobia, según aplicación. Sobre dicho soporte crece una biopelícula con un actividad mirificante elevada que apenas varía con la carga orgánica y condiciones de operación.5. Reactor according to claims 1 and 4, characterized by a rough granular support of high density polyethylene plastic or plastic material with equivalent characteristics-, with a density of 5 to 15% less than that of water, size between 1.5 and 5 mm. The volume of the support, located in the aerobic chamber, will be between 15 and 25% v / v, referred to the volume of the aerobic chamber, depending on the application. On this support grows a biofilm with a high mirifying activity that hardly varies with the organic load and operating conditions.
6.- Reactor, según las reivindicaciones 1, 4 y 5, caracterizado por un dispositivo de separación entre el licor de mezcla y el soporte granular plástico: El dispositivo se ubica por debajo de la parrilla de difusores de la cámara aerobia, y se encuentra anexo a la cámara de filtración. El dispositivo, en uno de sus lados, está dotado de un pozo de sección rectangular, y en otro de sus lados tiene una pendiente de la solera comprendida entre 20 y 45°. El dispositivo dispone de un tubo que comunica el pozo de la cámara aerobia con otro pozo similar ubicado en la cámara de filtración (3). El tubo tiene un extremo cerrado (en la cámara aerobia) y otro abierto (hacia la cámara de filtración) y posee una ranura longitudinal abierta y orientada hacia abajo en el pozó de la cámara aerobia.6. Reactor according to claims 1, 4 and 5, characterized by a separation device between the mixing liquor and the plastic granular support: The device is located below the diffuser grill of the aerobic chamber, and is located Annex to the filtration chamber. The device, on one of its sides, is equipped with a well of rectangular section, and on another of its sides it has a slope of the hearth between 20 and 45 °. The device has a tube that communicates the well of the aerobic chamber with another similar well located in the filtration chamber (3). The tube has a closed end (in the aerobic chamber) and an open end (towards the filtration chamber) and has an open longitudinal groove oriented downwards in the well of the aerobic chamber.
7.- Reactor, según la reivindicación 1, caracterizado porqué la cámara de filtración (3) está dotada de módulos de ultrafiltración o microfiltración de membranas de fibras huecas, fabricadas en polisulfonas, polipropileno o cualquier otro polímero adecuado. Dichos módulos irán montados en casetes o estructuras rectangulares dotadas de sistemas de limpieza de membranas adecuados, mediante corriente de aire, retro lavado con permeado o cualquier otro sistema que recomiende el fabricante de los módulos de filtración de membranas, y que sea compatible con la aplicación. El agua residual depurada se filtra con ayuda de una o más bombas centrífugas conectadas a los módulos de filtración de membranas. Se recomienda el uso de módulos de filtración de membranas ZeeWeed® de la casa Zenon Environmental Inc. o equivalentes. La cámara de filtración se dotará con una línea de purga de fangos, que consiste de una conducción conectada a una bomba, a través de la cual se purga periódicamente el lodo generado. La cámara de filtración dispondrá de un impulsor de flujo horizontal, y de una conducción ubicada en un lateral de la cámara con un extremo enfrente del impulsor de flujo horizontal. 7. Reactor according to claim 1, characterized in that the filtration chamber (3) is equipped with ultrafiltration or microfiltration modules of hollow fiber membranes, made of polysulfones, polypropylene or any other suitable polymer. These modules will be mounted on cassettes or rectangular structures equipped with adequate membrane cleaning systems, by means of air flow, permeate backwashing or any other system recommended by the manufacturer of membrane filtration modules, and that is compatible with the application . The purified waste water is filtered using one or more centrifugal pumps connected to the membrane filtration modules. The use of ZeeWeed ® membrane filtration modules from Zenon Environmental Inc. or equivalent is recommended. The filtration chamber will be equipped with a sludge purge line, which consists of a conduit connected to a pump, through which the generated sludge is periodically purged. The filtration chamber will have a horizontal flow impeller, and a conduit located on one side of the chamber with one end opposite the horizontal flow impeller.
8.- Reactor, según las reivindicaciones 1, 2 y 7, caracterizado por un dispositivo de recirculación de fangos desde la cámara de filtración de membranas (3) hacia la cámara anóxica (1), constituido por un impulsor de flujo horizontal enfrentado a un extremo de una conducción ubicada en un lateral de la cámara anóxica, que conecta ésta a un canal rectangular instalado en uno de los laterales superiores del reactor. El canal rectangular se prolonga desde la cámara de filtración hasta la cámara anóxica y dispone de un rebosadero anexo a la cámara anóxica. El licor de mezcla o lodo retenido en la cámara de filtración se recircula, utilizando el impulsor de flujo horizontal que conduce el lodo por la conducción hacia el canal de recirculación. El licor de mezcla retorna a la cámara anóxica a través del rebosadero ubicado en el canal de recirculación. 8. Reactor according to claims 1, 2 and 7, characterized by a sludge recirculation device from the membrane filtration chamber (3) to the anoxic chamber (1), constituted by a horizontal flow impeller facing a end of a conduit located on one side of the anoxic chamber, which connects it to a rectangular channel installed on one of the upper sides of the reactor. The rectangular channel extends from the filtration chamber to the anoxic chamber and has an overflow attached to the anoxic chamber. The mixing liquor or sludge retained in the filtration chamber is recirculated, using the horizontal flow impeller that conducts the sludge by conduction to the recirculation channel. The mixing liquor returns to the anoxic chamber through the overflow located in the recirculation channel.
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ES2401445B2 (en) * 2013-02-01 2014-01-20 Universidade De Santiago De Compostela Integrated system of anaerobic methanogenic reactor and membrane bioreactor for the elimination of organic matter and nitrogen in wastewater
CN103341285B (en) * 2013-07-16 2015-04-15 哈尔滨工业大学 Advection sedimentation/immersion type ultrafiltration integrated water treatment device
EP3197837A1 (en) * 2014-09-26 2017-08-02 Van Der Ende Pompen B.V. Method and system for treating a fluid flow
CN104407100B (en) * 2014-10-31 2016-08-17 北京城市排水集团有限责任公司 A kind of analysis method of mud nitrification activity intelligent analysis system
RU2608527C2 (en) * 2015-06-17 2017-01-19 Публичное акционерное общество "Газпром" Biocomposite for purification of waste water from nitrite-, nitrate-, phosphate ions
CN105087451B (en) * 2015-10-08 2018-07-10 南京大学 A kind of preparation method of denitrification microorganism microbial inoculum
CN112174352A (en) * 2020-08-25 2021-01-05 南京汉尔斯生物科技有限公司 Energy-saving anti-blocking drainage pool and use method thereof
WO2022167702A1 (en) 2021-02-02 2022-08-11 Biologia Y Filtracion, S.L. Industrial and municipal wastewater treatment plant

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4122013A (en) * 1977-11-15 1978-10-24 Greenleaf Jr John W Sewage treatment system
EP0002115A1 (en) * 1977-11-11 1979-05-30 Thetford Corporation Closed loop waste treatment and water recycling toilet system and method of operation
US4904387A (en) * 1988-06-17 1990-02-27 Thetford Corporation Waste treatment and water recycling toilet system
ES2097528T3 (en) * 1992-08-10 1997-04-01 Protec Partner Umwelttech PROCEDURE AND DEVICE FOR THE BIOLOGICAL TREATMENT OF WASTEWATER WITH ORGANIC LOAD AND ORGANIC WASTE.
WO2001005715A1 (en) * 1999-07-20 2001-01-25 Zenon Environmental Inc. Biological process for removing phosphorus involving a membrane filter
WO2001072644A1 (en) * 2000-03-29 2001-10-04 Ecokasa Incorporated Nitrogen reduction wastewater treatment system

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0002115A1 (en) * 1977-11-11 1979-05-30 Thetford Corporation Closed loop waste treatment and water recycling toilet system and method of operation
US4122013A (en) * 1977-11-15 1978-10-24 Greenleaf Jr John W Sewage treatment system
US4904387A (en) * 1988-06-17 1990-02-27 Thetford Corporation Waste treatment and water recycling toilet system
ES2097528T3 (en) * 1992-08-10 1997-04-01 Protec Partner Umwelttech PROCEDURE AND DEVICE FOR THE BIOLOGICAL TREATMENT OF WASTEWATER WITH ORGANIC LOAD AND ORGANIC WASTE.
WO2001005715A1 (en) * 1999-07-20 2001-01-25 Zenon Environmental Inc. Biological process for removing phosphorus involving a membrane filter
WO2001072644A1 (en) * 2000-03-29 2001-10-04 Ecokasa Incorporated Nitrogen reduction wastewater treatment system

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1747058A2 (en) * 2004-04-22 2007-01-31 US Filter Wastewater Group, Inc. Filtration apparatus comprising a membrane bioreactor and a treatment vessel for digesting organic materials
EP1747058A4 (en) * 2004-04-22 2009-09-30 Siemens Water Tech Corp Filtration apparatus comprising a membrane bioreactor and a treatment vessel for digesting organic materials
US7718065B2 (en) 2004-04-22 2010-05-18 Siemens Water Technologies Corp. Filtration method and apparatus
US7147777B1 (en) * 2005-05-09 2006-12-12 Eimco Water Technologies Llc Wastewater treatment system with membrane separators and provision for storm flow conditions
CN100357197C (en) * 2006-01-12 2007-12-26 上海大学 Integral membrane biological reaction device for water treatment
CN102120680A (en) * 2011-04-15 2011-07-13 龙江环保集团股份有限公司 Anoxic/oxic-membrane bioreactor water treatment device and sewage treatment method thereof
CN102120680B (en) * 2011-04-15 2012-10-03 龙江环保集团股份有限公司 Anoxic/oxic-membrane bioreactor water treatment device and sewage treatment method thereof
CN107619105A (en) * 2016-07-15 2018-01-23 深圳市深水生态环境技术有限公司 River channel ecology processing system and the smelly water body treating biofilm reactor of urban black
DE202017107020U1 (en) 2016-11-30 2017-11-29 ALVEST Group s.r.o Biological sewage treatment plant
CN118026408A (en) * 2024-04-11 2024-05-14 四川发展环境科学技术研究院有限公司 System and method for removing nitrogen and phosphorus in sewage by iron ion driven denitrification-anaerobic ammoxidation

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